JPH02302402A - Production of polymer particle - Google Patents

Abstract

PURPOSE:To obtain polymer particles having narrow particle size distribution in high reproducibility from variability of particle size distribution of polymer particles by dispersing and polymerizing a polymerizable monomer in the presence of a dispersant comprising a specific copolymer under a specific stirring condition. CONSTITUTION:A polymerizable monomer (preferably styrene) is dispersed and polymerized under a stirring condition of 0.005 to 0.30kw/m<2> PV value in the presence of a dispersant [preferably graft copolymer of (meth)acrylic acid alkyl ester, (meth)acrylic acid, a macromonomer shown by formula I (R<1> is H or methyl; R<2> and R<3> are 1 to 5C alkylene; (m) and (n) are 5 to 1,000) and a fluorine-containing monomer shown by formula II (q is 1 to 8)] comprising a copolymer having a hydrophilic segment, a perfluoroalkyl group and a hydroxylic group to give the aimed particles.

Description

DETAILED DESCRIPTION OF THE INVENTION Technical Field of the Invention The present invention relates to a method capable of producing polymer particles of uniform particle size with good reproducibility.

Technical background of the invention Polymer particles (spherical monodisperse polymer particles) with a particle size in the range of 1.0 to 10 μm, narrow particle size distribution, and uniform particle size can be used in toners, toner additives, paints, and adhesives. agent,
It is widely used as a textile treatment agent, cosmetic additive, or medical diagnostic additive.

Such spherical monodisperse polymer particles can be produced by methods such as dispersion polymerization, suspension polymerization, emulsion polymerization, and soap-free emulsion polymerization.

Among these manufacturing methods, the dispersion polymerization method has the advantage that the polymerization operation is very simple, as the raw materials are charged all at once and polymerization is performed in a homogeneous system, and it is possible to produce monodisperse polymer particles. It is suitable as a method for

However, for monodisperse polymer particles produced using the dispersion polymerization method, the particle size of the resulting polymer particles changes significantly depending on the polymerization conditions, and when trying to obtain polymer particles with a narrow particle size distribution, the polymerization conditions must be set. is very difficult. In particular, even if it is possible to produce polymer particles with a very narrow particle size distribution at the laboratory level, when scaled up to an industrial scale, the reaction set up at the laboratory level as described above Even if the conditions were applied as they were, it was generally not possible to obtain polymer particles having the same particle size distribution. It is not clear which reaction conditions among the various reaction conditions act as a factor that determines the particle size distribution. Therefore, when changing the production scale, preliminary polymerization There was a problem in that it was necessary to carry out the procedure to set suitable polymerization conditions again, and the operation was very complicated. Moreover, the particle size distribution of polymer particles polymerized under the polymerization conditions set in this way tends to fluctuate, and polymer particles with different particle size distributions are often obtained each time they are manufactured, resulting in very poor reproducibility. There was a problem.

Purpose of the Invention The present invention aims to solve the problems of the prior art as described above, and aims to provide a method that can produce monodisperse polymer particles with a narrow particle size distribution with good reproducibility. It is said that

Summary of the Invention The method for producing polymer particles according to the present invention comprises adding a polymerizable monomer to a Pv value of 0.005 in the presence of a dispersant comprising a copolymer having a hydrophilic segment, a perfluoroalkyl group, and a hydrophilic group. It is characterized by carrying out dispersion polymerization under stirring conditions of ~0.30 Kw/rd.

According to the method for producing polymer particles according to the present invention, a dispersant made of a specific graft polymer is used and the polymerization reaction is carried out under specific stirring conditions. Polymer particles with a narrow particle size distribution and less variation in particle size distribution can be produced with good reproducibility.

Detailed Description of the Invention Next, the method for producing polymer particles of the present invention will be specifically described.

In the method for producing polymer particles of the present invention, polymerizable monomers are dispersed and polymerized under specific stirring conditions in the presence of a specific dispersant.

The dispersant used in the present invention is a copolymer having a hydrophilic segment, a perfluoroalkyl group, and a hydrophilic group.

The above copolymers are composed of a monomer having a hydrophilic segment and a reactive double bond, a monomer having a perfluoroalkyl group and a reactive double bond, and a monomer having a hydrophilic group and a reactive double bond. It can be obtained by copolymerizing a monomer with a bond.

A monomer having a hydrophilic segment and a reactive double bond (in the present invention, this compound is referred to as a "macromonomer") used to produce such a copolymer usually has a molecular weight of 1,000 to 1,000. 100000, preferably 30
00 to 50,000. Therefore, there are usually 10 to 1000, preferably 30 to 1000, in this hydrophilic segment.
Contains 500 hydrophilic groups.

Examples of the hydrophilic groups contained in the hydrophilic segment include hydroxyl groups, carboxyl groups, alkali metal salts thereof, amine salts thereof, ammonium salts thereof, sulfone groups,
Mention may be made of the amine salts thereof, the ammonium salts thereof, and groups derived from basic nitrogen-containing vinyl monomers of the formula, such as dialkylaminoalkyl (meth)acrylates.

However, in the above formula, R11 represents a hydrogen atom or an alkyl group having 1 to 5 carbon atoms, R12 and R13 each independently represent a hydrogen atom or an alkyl group having 1 to 6 carbon atoms, and n represents a hydrogen atom or an alkyl group having 1 to 6 carbon atoms. is an integer.

As such a macromonomer, a compound containing a predetermined amount of the above-mentioned hydrophilic groups and having a reactive double bond can be used. Particularly in the present invention, it is preferable to use a compound represented by the following formula [I] as the macromonomer.

(2) CH2-C-R C'-0 ... [I] However, in the above formula [I], R1 each independently represents a hydrogen atom or a methyl group.

It is particularly preferred that R1 is a methyl group. Further, R2 and R3 usually each independently have a carbon number of 1 to 5,
In particular, R2 is preferably 1 to 2 alkyl groups,
Further, R3 is preferably 1 to 2 alkyl groups. In the above formula [I1, m represents 5 to 1000 and n represents 5 to 1000. The ratio (mn) of m and n is usually in the range of 1:200 to 200:1, preferably 1:10 to 10:1.

For example, the macromonomer described above is prepared by first polymerizing an ethylenically unsaturated monomer in the presence of a reaction initiator to prepare an addition type polymer having a terminal functional group capable of condensation reaction, and then polymerizing this addition type monomer. It can be produced by a method in which a vinyl group is introduced into the terminal by reacting an epoxy compound having a vinyl group at the terminal.

Examples of ethylenically unsaturated monomers used to produce the above macromonomers include (meth)acrylamide and its derivatives; N-methylol (meth)acrylamide and its derivatives; diacetone (meth)acrylamide and its derivatives. ; Hydroxyalkyl (meth)acrylates and their derivatives such as hydroxyethyl (meth)acrylate, hydroxypropyl (meth)acrylate, hydroxybutyl (meth)acrylate; Polyhydric alcohols such as methyl triglycol (meth)acrylate ( Meth)acrylic acid ester and its derivatives; Vinylpyrrolidone and its derivatives; Ethyl carpitol (meth)acrylate and its derivatives; 2-hydroxyethyl acryloyl phosphate and its derivatives; 2-methoxyethyl (meth)acrylate, butoxyethyl (meth) ) acrylates such as alkoxyalkyl (meth)acrylates.

In addition, the epoxy compound used to introduce a vinyl group at the terminal can be appropriately selected from compounds having an epoxy group and a vinyl group.
Examples of such compounds include glycidyl (meth)acrylate, 2-methylglycidyl (meth)acrylate, arylglycidyl ether, and aryl-2-methylglycidyl ether.

The above macromonomers can be used alone or in combination.

In addition, the reaction initiators used in the above reaction include 4,4-azobis-4-cyanovaleric acid, 2,2
Common initiators such as °-amidinopropanoate, potassium peroxide, ammonium peroxide, azobisisobutyronitrile, benzoyl peroxide can be used.

The content of the above-mentioned macromonomer in the copolymer as a dispersant is usually 1 to 30% by weight, preferably 5 to 20% by weight.
Weight%.

Examples of monomers having a fluoroalkyl group and a reactive double bond (referred to as "fluorine-containing monomers" in the present invention) used in the preparation of the copolymer used as a dispersant in the present invention include: , trifluoroethyl (meth)acrylate, 3-[(+
)-octadecylfluoro)-2-oxybenzoyloxy]-2-hydroxypropyl (meth)acrylate, 3-methyl-4-[perfluoro(7-methyl-1-octyl)]butyl (meth)acrylate, 2-( N, N
-propyl perfluorooctyl sulfonamido)ethyl (meth)acrylate, 2-(perfluorooctylethyl (meth)acrylate, 3.3.3-)lifluoropropylene (meth)acrylate, hexafluoropropylene (meth)acrylate, difluoro Mention may be made of hexafluorobutene-2-(meth)acrylate.

Further, as such a fluorine-containing monomer, a compound represented by the following formula can also be used.

CF3CF-(CF2). C112CIl-CI+ 2-
OCO-C-CI+2CF-(CF2). -3O2
N-(C11゜') I, 1-OCO-C-CI+□However, in the above formula, R1 is a hydrogen atom, -CH,
-CHF, -CH2F or -R represents a hydrogen atom or -CH3.

In the present invention, the above-mentioned fluorine-containing monomer is preferably a monomer having a perfluoroalkyl group, and among these seven monomers, the following formula [I
Particularly preferred are compounds represented by 1.

CH-CR1COOR2CF 2 q 2q+1...[I
I] However, in the above formula [I], R1 represents a hydrogen atom or a methyl group, and is particularly preferably a methyl group. Further, R2 usually represents an alkylene group having 1 to 5 carbon atoms, preferably an alkylene group having 1 to 2 carbon atoms.

And q in the above formula [I1] is usually an integer of 1 to 8, preferably an integer of 3 to 8.

Note that the above fluorine-containing monomers can be used alone or in combination.

The content of the above-mentioned fluorine-containing monomer in the copolymer as a dispersant is usually 1 to 40% by weight, preferably 10% by weight.
~30% by weight.

Further, the monomer having a hydrophilic group and a reactive double bond used to produce the copolymer which is the dispersant of the present invention includes a carboxyl group, a sulfonic group, and an alkali metal salt or amine salt thereof. , a compound having a hydrophilic group such as an ammonium salt.

Examples of such compounds include (meth)acrylic acid,
Unsaturated monocarboxylic acids such as crotonic acid, isocrotonic acid, vinyl acetic acid, angelic acid, tiglic acid, allyl acid; unsaturated dicarboxylic acids such as maleic acid, fumaric acid, citraconic acid, methyl fumaric acid, glutaconic acid, itaconic acid, allylmalonic acid acids; or monoalkyl esters of dicarboxylic acids; 2-acrylamido-2-methylpropanesulfonic acid, vinylsulfonic acid, allylsulfonic acid, 2-methylallylsulfonic acid, styrenesulfonic acid, (meth)acrylic acid-2
-sulfoethyl, -2-sulfopropyl (meth)acrylate, etc. and the acceptable salts of the above-mentioned compounds.

Particularly in the present invention, it is preferable to use methacrylic acid.

These compounds that bind hydrophilic groups and reactive double bonds can be used alone or in combination.

The content of the above-mentioned monomer having a hydrophilic group in the copolymer as a dispersant is usually 1 to 30% by weight, preferably 5 to 20% by weight.

In the present invention, the copolymer used as a dispersant is
Any copolymer of monomer components such as those mentioned above may be used.
Furthermore, it is usually obtained by copolymerizing a non-hydrophilic monomer such as alkyl (meth)acrylate.

Examples of such non-hydrophilic monomers include styrene, vinyltoluene, α-methylstyrene,
Aromatic vinyl monomers such as chlorostyrene, conjugated diene monomers such as butadiene, isoprene, chlorobrene,
(meth)acrylic acid esters such as methyl (meth)acrylate, ethyl (meth)acrylate, propyl (meth)acrylate, butyl (meth)acrylate, vinyl chloride,
Mention may be made of vinyl halides such as vinyl bromide and vinylidene chloride and vinyl esters such as vinylidene, vinyl acetate and vinyl propionate.

These monomers can be used alone or in combination.

The content of the monomer having no hydrophilic group in the copolymer as a dispersant is usually 10 to 80% by weight, preferably 30 to 60% by weight.

The graft copolymer used as a dispersant in the present invention is
The above-mentioned macromonomer, fluorine-containing monomer, monomer having a hydrophilic group, and optionally a monomer having no hydrophilic group can be produced by graft polymerization using a known method. Polymerization methods that can be used for this graft polymerization include emulsion polymerization,
There are methods such as suspension polymerization method and dispersion polymerization method.

The molecular weight of the graft copolymer produced using such a polymerization method is usually in the range of 5,000 to 300,000, preferably 10,000 to 100,000.

Since the copolymer described above has a hydrophilic group in a hydrophilic segment and a side chain, it can be dissolved in an alcohol/cellosolve mixed solvent that is preferably used in the method for producing polymer particles of the present invention. It serves as a good dispersant for the resulting polymer particles.

In the method for producing polymer particles of the present invention using a dispersant as described above, various monomers can be used as the polymerizable monomer used to produce the polymer particles.

Examples of such heavy monomers include aromatic vinyl monomers such as styrene, vinyltoluene, α-methylstyrene, and chlorostyrene; conjugated diene monomers such as butadiene, isoprene, and chlorobrene; and methyl (meth)acrylate. (meth)acrylic acid alkyl esters such as ethyl (meth)acrylate, propyl (meth)acrylate, butyl (meth)acrylate; vinyl halides such as vinyl chloride, vinyl bromide, vinylidene chloride, vinylidene bromide; Vinylidene halide: Vinyl esters such as vinyl acetate and vinyl propionate can be mentioned.

Particularly in the present invention, the polymerizable monomer is preferably one containing styrene as a main component, and in this case, the content of styrene in the polymerizable monomer is 50 mol% or more, preferably 60 mol% or more. This is desirable.

Such a dispersion polymerization reaction is usually carried out in an organic solvent. As the solvent used in this reaction, it is preferable to use a mixed solvent of alcohol and cellosolve solvent. As the alcohol that can be used in this case, it is preferable to use an alcohol having 1 to 5 carbon atoms such as methanol, ethanol, and isopropanol, and as the cellosolve solvent, methyl cellosolve, ethyl cellosolve, isopropyl It is preferable to use a cellosolve-based solvent having an alkyl group having 1 to 4 carbon atoms, such as cellosolve and butyl cellosolve.

Among such mixed solvents of alcohol and cellosolve-based solvents, a mixed solvent of methanol and methyl cellosolve, a mixed solvent of ethanol and methyl cellosolve, and a mixed solvent of isopropanol and methyl cellosolve may be used. Preference is given to using a solvent.

Such a mixed solvent is usually 200 to 2000 parts by weight, preferably 25 parts by weight, per 100 parts by weight of the polymerizable monomer.
It is used in an amount of 0 to 1000 parts by weight.

In the production method of the present invention, the average particle diameter of the obtained polymer particles can be controlled by changing the mixing ratio of alcohol and cellosolve solvent.

For example, Figure 1 shows an example of the influence of the solvent composition on the particle size when styrene is used as the polymerizable monomer, methyl cellosolve is used as the cellosolve solvent, and methanol, ethanol, or isopropanol is used as the alcohol. Shown below.

That is, in the example shown in FIG. 1, the ratio of the total weight of alcohol, cellosolve solvent, and styrene is fixed at 335:100, and the mixing ratio of alcohol, cellosolve solvent, and styrene to the total weight is varied. As a result, the average particle diameter of the resulting polymer particles changes.

Furthermore, it is easier to control the average particle size of polymer particles when ethanol is used than when isopropanol is used as the alcohol, and by using methanol, it is even easier to control this average particle size. become. That is, there is a tendency that the use of an alcohol with fewer carbon atoms makes it easier to control the average particle diameter of the resulting polymer particles.

In the present invention, when dispersing and polymerizing the polymerizable monomer using the above-mentioned dispersant, it is necessary to perform stirring under specific conditions. That is, in the dispersion polymerization system as described above, the particle diameter of the resulting polymer particles varies significantly depending on the stirring conditions. Furthermore, the stirring conditions are the main factor determining the average particle size of the resulting polymer particles. Therefore, by specifying this stirring condition, the particle size of the obtained polymer particles can be specified, and furthermore, the particle size of the obtained polymer particles is less likely to fluctuate due to scale-up.

In the present invention, it is necessary to set the Pv value during stirring in the above-mentioned dispersion polymerization system within the range of 0.005 to 0.30 Kw/rrt, and furthermore, this Pv value must be set to 0.005 to 0.30 Kw/rrt.
01~0. It is preferable to set it within the range of 15 Kv/n.

Here, the Pv value is expressed by the following formula.

ω・T vm - ■ In addition, in the above formula, ω・・・Stirring speed T...Stirring torque ■・・・Reaction capacity represents.

FIG. 2 shows an example of the relationship between the Pv value, the average particle diameter of the resulting polymer particles, and the Cv value of the polymer particles.

Pv value of 0.005 to 0.3 at 10g production scale
0Kw/rr? By keeping it within the range of about 1 to 10
Polystyrene particles having an average particle diameter of .mu.m can be obtained, and the polystyrene particles produced under such conditions have a Cv value within the range of 1 to 3% and have extremely uniform particle diameters.

It can be seen that even when the production scale is scaled up to 400 g, the average particle diameter and Cv value are equivalent to the average particle diameter and Cv value of the polymer particles produced on the ION production scale.

Furthermore, by setting the Pv value within the range of 0.01 to 0.15 Kw/n, it becomes particularly easy to produce polymer particles with uniform particle diameters.

Such a Pv value can be controlled by changing the stirring torque and stirring speed in a given reaction vessel as described above. In other words, by changing the stirring power, the size or shape of the stirring blades, and by changing the stirring torque and stirring speed, P
v value can be controlled.

In dispersion polymerization carried out under such stirring conditions, the temperature conditions are usually set within the range of 50 to 80°C. Furthermore, it is preferable to set the temperature within the range of 60 to 75°C. Further, it is preferable that the temperature fluctuation range is small, and usually this temperature fluctuation range is 0.1 to 2°C, preferably 0.1°C.
Controlled within the range of ~0.5°C.

Furthermore, in the present invention, this reaction can also be carried out in two stages. However, it is preferable that the temperature fluctuation range in each stage is small, and it is particularly preferable that the temperature fluctuation range is set to the above-mentioned temperature fluctuation range.

The reaction time in the present invention can be appropriately set in consideration of the amount of monomers used, reaction conditions, etc., but is usually 5 to 30 hours, preferably 7 to 24 hours.

FIG. 3 shows an example of the relationship between reaction time and temperature when the reaction is carried out in two stages. Figure 3 shows rBPO
J indicates the point at which benzoyl peroxide, which is a reaction initiator, is added, and the reaction substantially starts from this point.

In FIG. 3, the reaction was carried out at 70°C for 2 hours and then at 75°C for 6.5 hours.

FIG. 4 shows an electron micrograph of the polymer particles obtained by reacting in this manner. As is clear from FIG. 4, by dividing the reaction into two stages to produce the polymer particles of the present invention as described above, it is possible to produce polymer particles with extremely uniform particle diameters.

The polymer particles thus obtained can be obtained by removing the dispersant using a method such as filtration or centrifugation, and then drying.

Effects of the Invention According to the method for producing polymer particles according to the present invention, a dispersant made of a specific graft polymer is used and the polymerization reaction is carried out under specific stirring conditions. The particle size distribution of the polymer particles is less likely to fluctuate, and polymer particles having a narrow particle size distribution can be produced with good reproducibility.

Next, the present invention will be described with reference to Examples, but the present invention should not be construed as limited by these Examples.

In addition, in the examples and comparative examples shown below, 1
The expression "parts" means "parts by weight" unless otherwise specified.

Dispersant Production Example 1 In a 1 g 4-day flask equipped with a reflux condenser, a thermometer, a nitrogen blowing tube, and a mixing device, 300 parts of methyl ethyl ketone and 300 parts of a monomer mixture according to the composition shown in Table 1 were added. , azobisisobutyronitrile 1.
5 parts were added and kept at 70±2° C. for 8 hours under a nitrogen stream to complete graft polymerization.

Next, the obtained polymer was poured into methanol to precipitate it, and it was dried to obtain a powder, thereby obtaining a dispersant (A).

Dispersant Production Examples 2 to 4 Dispersant (B),
(C) and (D) were obtained.

Dispersant Production Comparative Example 1 In a 1N40 flask equipped with a reflux condenser, a thermometer, a nitrogen blowing tube, and a mixing device, 300 parts of methyl ethyl ketone was added instead of 60 parts of N-methylolacrylamide macromer listed in Table 1. , 60 parts of N-methylolacrylamide were blended, other conditions were the same as in Production Example 1, and a dispersant (
A) was obtained.

Dispersant Production Comparative Example 2 Into a 1FF40 flask equipped with a reflux condenser, thermometer, nitrogen blowing tube, and a mixing device, 300 parts of methyl ethyl ketone and 2-(perfluorooctyl)-ethyl methacrylate listed in Table 1 were added. A dispersant (b) was obtained in the same manner as in Production Example 1, except that 90 parts of decyl methacrylate was added instead of 90 parts, and the other conditions were the same as in Production Example 1.

Example 1 In a 1 g reaction vessel equipped with a reflux condenser, a thermometer, a nitrogen inlet tube, and a stirrer with a torque meter, 183 parts of ethanol, 152 parts of methyl cellosolve, 100 parts of styrene (ST),
Add 10 parts of the dispersant (A) synthesized in Dispersant Production Example 1,
Stirring was performed under a nitrogen stream at a pv value of 0.017 KW/nf.

Next, the temperature of the reaction solution was raised to 70°C, and when it reached 70°C, benzoyl peroxide (BPO) was added as a polymerization initiator.
3 parts were added to initiate polymerization.

After the temperature of the reaction solution was maintained at 70° C. and the reaction was carried out for 2 hours, the temperature of the reaction solution was raised to 75° C., and polymerization was further carried out for 6 hours.

The resulting polymer dispersion was filtered through a 200-mesh wire mesh, but almost no aggregates were observed.

When the obtained polymer particles were observed with a scanning electron microscope, monodisperse polystyrene particles of 4.6 microns and a CV value of 2.3% were obtained.

Examples 2 to 4 In Example 1, dispersants (B), (C) and (D) prepared in Dispersant Production Examples 2 to 4 were used instead of dispersant (A).
) Dispersion polymerization of styrene was carried out in the same manner except that the following was used.

The properties of the obtained polymer particles are shown in Table 2.

All polymer particles were monodisperse particles.

Table 2 Examples 5 to 7 Dispersion polymerization of styrene was carried out in the same manner as in Example 1 except that the stirring conditions were changed to pv value of 0.005 KW/I, pv value of 0.5 KW/I, and 0.15 KW/G. .

Table 3 shows the properties of the obtained polymer particles.

Table 3 Examples 8 to 10 In Example 1, the type and amount of alcohol used as the polymerization solvent were changed to 183 parts of ethanol and 152 parts of methylcellosolve (
Example 8) 183 parts of methanol and 152 parts of methylcellosolve (
Dispersion polymerization of styrene was carried out in the same manner as in Example 9), except that 248 parts of isopropyl alcohol and 87 parts of methylcellosolve (Example 10) were used.

Table 4 shows the properties of the obtained polymer particles.

Table 4 Comparative Example 1 In Example 1, the dispersant (
Instead of A), the dispersant (
b) Dispersion polymerization of styrene was carried out in the same manner except that 10 parts was used.

The average particle size of the obtained polymer particles was 5.5 microns and C
A particle with a V value of 6% and a wide particle size distribution was obtained.

Comparative Example 2 In Example 1, the dispersant (
Instead of A), the dispersant (
b) Dispersion polymerization of styrene was carried out in the same manner except that 10 parts was used.

The average particle size of the obtained polymer particles was 4.6 microns and Cv
A value of 7% and a wide particle size distribution were obtained.

Comparative Example 3 In Example 1, the stirring condition Pv value was 0.018.
Dispersion polymerization of styrene was carried out under the same stirring conditions except that the Pv value was changed to 0.7 KW/ri''.

The average particle size of the obtained polymer particles was 9 μm and the CV value was 11%.
A fairly wide particle size distribution was obtained.

Comparative Example 6 In Example 1, the stirring condition Pv value was 0.018.
Dispersion polymerization of styrene was carried out under the same stirring conditions except that KW/rrr was changed to a Pv value of 0.002 KW/a.

The average particle size of the obtained polymer particles was 3.7 μm, and the CV value was 3.
．． A slightly broader particle size distribution of 5% was obtained.

[Brief explanation of the drawing]

FIG. 1 is a graph showing an example of the influence of solvent composition on particle size. FIG. 2 is a graph showing an example of the relationship between the Pv value and the average particle diameter and Cv value of the resulting polymer particles. FIG. 3 is a graph showing an example of the relationship between reaction time and temperature. FIG. 4 is an example of an electron micrograph showing the particle structure of polymer particles obtained by the method of the present invention. Agent Patent attorney Shunichi Suzuki Figure 1 [MeOH, EtOH, IPA + [5tl=335:100 Reaction temperature

Claims (5)

[Claims] (1) In the presence of a dispersant consisting of a copolymer having a hydrophilic segment, a perfluoroalkyl group, and a hydrophilic group, a polymerizable monomer is added with a Pv value of 0.005 to 0.30 Kw.
A method for producing polymer particles, characterized by carrying out dispersion polymerization under stirring conditions of /m^2. (2) The method for producing polymer particles according to claim 1, wherein the main component of the polymerizable monomer is styrene. (3) The dispersant is a graft combination of (meth)acrylic acid alkyl ester, (meth)acrylic acid, a macromonomer represented by the following formula [I], and a fluorine-containing monomer represented by the following formula [II]. A method for producing polymer particles according to claim 1, which is a polymer; ▲There are mathematical formulas, chemical formulas, tables, etc.▼... [I] (However, in the above formula [I], R^ 1 each independently represents a hydrogen atom or a methyl group, R^2 and R^3 each independently represent an alkylene group having 1 to 5 carbon atoms, m is 5 to 1000, and n is 5 to 100
0), CH_2=CR^1COOR^2C_qF_2_q_+
_1...[II] (However, in the above formula [II], R
^1 represents a hydrogen atom or a methyl group, R^2 represents an alkylene group having 1 to 5 carbon atoms, and q represents 1 to 8
). (4) The method for producing polymer particles according to claim 1, wherein the dispersion polymerization is carried out in a mixed solvent of alcohol and cellosolve solvent. (5) The method for producing polymer particles according to claim 4, wherein the dispersion polymerization is carried out at a temperature within the range of 50 to 80°C.